WO2004085040A2 - Systeme et procede de membrane a precipitation preferentielle - Google Patents

Systeme et procede de membrane a precipitation preferentielle Download PDF

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Publication number
WO2004085040A2
WO2004085040A2 PCT/US2004/009055 US2004009055W WO2004085040A2 WO 2004085040 A2 WO2004085040 A2 WO 2004085040A2 US 2004009055 W US2004009055 W US 2004009055W WO 2004085040 A2 WO2004085040 A2 WO 2004085040A2
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WO
WIPO (PCT)
Prior art keywords
semi
solution
pressure side
stream
permeable membrane
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Application number
PCT/US2004/009055
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English (en)
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WO2004085040A3 (fr
WO2004085040A8 (fr
Inventor
Ronald J. Enzweiler
Peter Allan
Jurgen Heinz Strasser
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Itt Manufacturing Enterprises, Inc.
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Application filed by Itt Manufacturing Enterprises, Inc. filed Critical Itt Manufacturing Enterprises, Inc.
Publication of WO2004085040A2 publication Critical patent/WO2004085040A2/fr
Publication of WO2004085040A3 publication Critical patent/WO2004085040A3/fr
Publication of WO2004085040A8 publication Critical patent/WO2004085040A8/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/029—Multistep processes comprising different kinds of membrane processes selected from reverse osmosis, hyperfiltration or nanofiltration
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the present invention relates to water treatment and, more specifically, to a method and system of removing solutes from an aqueous solution containing a high level of sparingly soluble inorganic solutes.
  • the purity of the feed stream is usually limited by one or more sparingly soluble constituents in the feed stream, or by the inability of the soluble or sparingly soluble constituents to stay in solution as the concentration of the sparingly soluble constituents increases on the high pressure side of the membrane.
  • a fraction of the soluble or sparingly soluble constituents eventually precipitates out during the membrane separation process, resulting in a decrease in liquid that permeates the membrane.
  • antiscalants chemicals referred to as "antiscalants” have been added to the feed stream liquid prior to any reverse osmosis (RO) unit to increase the solubility of the sparingly soluble constituents.
  • RO reverse osmosis
  • the present invention is directed to a system and method for removing solutes from an aqueous solution containing a high level of sparingly soluble inorganic solutes (for example, but not limited to, a waste water stream) in a manner that achieves a high recovery rate of the water content of the solution, as well as a high removal rate of the solutes contained in the solution in an efficient, continuous flow membrane process.
  • the invention is particularly useful for producing product water with less than 500 mg/L of total dissolved solids (TDS) from initial feed streams containing between 3,000 and 20,000 mg/L of TDS with high levels of non-carbonate hardness (e.g., 1,000 to 2,500 mg/L of calcium and magnesium hardness expressed as calcium carbonate equivalents).
  • dissolved sparingly soluble constituents in the system feed stream are removed ahead of an RO membrane separation device by employing a separate first-pass nanofiltration (IMF) membrane.
  • IMF nanofiltration
  • One such method involves a first-pass NF membrane separation process to remove sparingly soluble constitutes from the feed-stream solution by providing, at startup, an effective amount of suitable seed nucleation crystals in the fluid stream introduced to the NF membrane unit.
  • seed nucleation crystals e.g., CaS0 4
  • the initial charge of seed nucleation crystals is the same material that is precipitated out of solution as the sparingly soluble solutes in the system feed stream (e.g., Ca 2+ ions and S0 4 2" ions) are concentrated.
  • the precipitation of the sparingly soluble solutes present in the system feed stream will occur upon the nucleation crystals, rather than on the membrane surface as mineral scale.
  • a means is provided to separate the retentate stream from the first-pass NF membrane process into (i) a discharge stream containing a minority of the nucleation crystals and water content of the NF retentate, and (ii) a recycle stream containing a majority of the nucleation crystals and water content of the NF retentate.
  • the discharge stream Before the discharge stream is discharged from the system, it may be further separated using a settling tank, hydrocyclone, or any other suitable solids/liquid separation device into (i) a fraction containing a higher level of suspended solids and (ii) a fraction containing a lower level of suspended solids.
  • NF retentate stream from the second-pass RO unit is also recycled, at least in part, to the feed stream of the NF unit.
  • Fig. 1 is a schematic representation of a high recovery, high rejection, double- pass membrane process for desalinating water containing soluble and sparingly soluble inorganic materials in which the nucleation crystals used to effect the preferential precipitation of the sparingly soluble inorganic material in the first-pass membrane unit are returned to, and reused in, the process;
  • Fig. 2 is a schematic representation of the same water desalination process shown in Fig.l but with the addition of means for recycling a majority fraction of the preferential precipitation nucleation crystals directly to the feed stream of the first-pass membrane unit;
  • Fig. 3 is a schematic representation of the same water desalination process shown in Fig.l but with the addition of bypassing the first-pass membrane unit with a fraction of the system feed stream and feeding the fraction directly into the second- pass membrane unit;
  • Fig. 4 is a schematic representation of the same water desalination process shown in Fig.l but with the addition of providing means for heating the feed stream before the feed stream enters the first-pass membrane unit;
  • Fig. 5 is a schematic representation of the same water desalination process shown in Fig.2 but with the addition of providing means for independently and instantaneously controlling the quantity of dissolved solids that leaves the system and the quantity of suspended solids that leaves the system so that steady-state operations can be maintained;
  • Fig. 6 is a schematic representation of the same water desalination process in shown Fig. 5 but with the addition of providing means for desuperaturating the solutions containing the nucleation crystals that are returned and reused to effect the preferential precipitation of the sparingly soluble solutes i n the system feed stream in the first-pass membrane unit; and
  • Fig. 7 is a schematic representation of the same water desalination process shown in Fig. 5 but with the addition of providing means for reducing the agronomic sodium adsorption ratio of the system product water.
  • first-pass membrane separation unit 33 is designated as a nanofiltration (NF) membrane
  • second-pass membrane separation unit 34 is designated as a reverse osmosis (RO) unit.
  • NF nanofiltration
  • RO reverse osmosis
  • liquid feed stream 1 to be purified e.g., hard water containing silica, calcium carbonate, calcium sulfate and suspended solids or wastewater or groundwater containing the same
  • liquid feed stream 1 to be purified is combined (i) with majority fraction stream 32 from the solids separation unit 8 containing a controlled amount of the nucleation crystals being returned to the process and (ii) with the retentate stream 13 from the second-pass membrane separation unit 34.
  • These three combined streams form stream 3 which is pressurized and fed to the high pressure side 4 of the first-pass membrane separation unit 33 [e.g., NF in this embodiment).
  • seed nucleation crystals 25 are added to the system so that a sufficient quantity of nucleation crystals are initially present in stream 3 to achieve the preferential precipitation of the sparingly soluble solutes in strea m 3 onto the nucleation crystals in the high pressure side 4 of the first-pass membrane separation unit 33.
  • the required level of seed nucleation crystals will be whatever is necessary given operating conditions, but typically might be up to 50 g/L, and preferably will range from 10 g/L to 40 g/L. This quantity can be determined in advance by experimentation.
  • the addition of nucleation crystals at startup can be made anywhere in the process (except streams 9, 14 and 15 in Fig. 1).
  • Fig. 1 shows the startup nucleation crystals being added into stream 32 as one possibility.
  • the feed stream 3 containing water, dissolved solids and nucleation crystals is conveyed to the high pressure side 4 of the first-pass membrane separation unit 33 wherein stream 3 is separated into a permeate stream 9 and a retentate stream 7.
  • the membrane 5 used in the first-pass membrane separation unit 33 is selected so that a higher percentage of the dissolved divalent ions in stream 3 are rejected and concentrated in stream 7 as compared to the percentage of monovalent ions that are rejected and concentrated in stream 7.
  • a relatively higher percentage of the dissolved monovalent ions than divalent ions pass through the membrane 5 into the permeate stream 9 from the first-pass membrane separation unit 33-
  • a nanofiltration membrane with a divalent ion rejection rating >80% and a TDS rejection rating >65% is used as the membrane(s) 5 in the first-pass membrane separation unit 33.
  • All suspended solids in stream 3, including the nucleation crystals, are rejected by membrane 5 and are present in the retentate stream 7 that leaves the high pressure side 4 of the first-pass membrane separation unit 33.
  • the mass of suspended solids increases on the high pressure side 4 of the first-pass membrane separation unit 33 because, as water permeates through membrane 5, the saturation limit of the rejected sparingly soluble inorganic solutes present in feed stream 3 is reached. This causes the solutes to precipitate out of solution on the high pressure side 4 of membrane 5. In this manner, the sparingly soluble solutes present in the system feed 1 are removed from solution without fouling first-pass membrane 5.
  • a preferred embodiment uses a polyamide thin film composite membrane in tubular construction for the first-pass membrane separation unit 33.
  • the recovery rate achieved in the first-pass membrane separation unit 33 is not limited by the potential for sparingly soluble solutes to precipitate out of solution and foul the membrane 5. On the basis of these factors, a recovery rate in the range of about 75% is generally the optimal recovery rate for the first-pass membrane separation unit 33, although higher rates could be achieved.
  • the retentate stream from the first-pass membrane separation unit 33 is conveyed along line 7 to a solids separation device 8.
  • the solids separation device 8 e.g., gravity settling tank, centrifuge, hydrocyclone or filter
  • minority fraction stream 15 is discharged from the system and majority fraction stream 32 is returned to the process as a component of feed stream 3 to the first-pass membrane separation unit 33.
  • the sum of the mass of solids leaving the desalination system in lesser fraction discharge stream 15 and in permeate stream 14 from the second-pass membrane separation unit 34 must be controlled to equal the mass of solids entering the desalination system as a part of feed stream 1.
  • a comminution device (not shown in Fig. 1), such as a shear mixer or gear pump, may be placed in majority fraction stream 32.
  • Permeate from the first-pass membrane separation unit 33 is conveyed along line 9 and becomes the feed (under some pressure) to the second-pass membrane separation unit 34.
  • the membrane 11 used in the second-pass membrane separation unit 34 is selected to achieve the desired level of purity of the product water stream 14.
  • a reverse osmosis class membrane with a TDS rejection rating of >95% is used in the second-pass membrane separation unit so product water with ⁇ 500 mg/L of TDS is produced.
  • the rate of production of permeate in the second-pass membrane separation unit 34 must be controlled to avoid precipitation of the sparingly soluble constituents in feed stream 9 on the high pressure side 10 of membrane 11. If the second-pass membrane separation unit 34 is operated at too great a recovery rate, precipitation of sparingly soluble solutes can occur on the high pressure side 10 of membrane 11. Because no nucleation crystals are present in stream 9, if the solubility limit of sparingly soluble solutes in stream 9 is reached as permeate 14 is produced on the low pressure side 12 of membrane 11, the precipitate that is produced can deposit on the membrane surface and foul the membrane 11. Thus, the recovery rate of second-pass membrane separation unit 34 must be controlled so as to avoid the precipitation of the sparingly soluble constituents in the feed stream 9 on the high pressure side 10 of membrane 11.
  • the retentate stream 13 from the second-pass membrane separation unit 34 is returned to form part of the feed stream 3 to the first-pass membrane separation unit 33.
  • overall recovery rates for the present desalination method of up to 99% can be achieved.
  • overall system recovery rates are generally limited to 90% to 95% (although not precisely) for feed streams containing between 5,000 and 15,000 mg/L TDS and product water TDS levels of ⁇ 500 mg/L.
  • FIG. 2 A second embodiment of the present invention is shown in Fig. 2.
  • This embodiment is the same water desalination method as shown in Fig. 1, but with the addition of splitting the retentate stream 7 from the high pressure side 4 of the first- pass membrane separation unit 33 into two fractions.
  • the first fraction stream 17 containing a majority (>50%) of the mass and volume flow rate of stream 7 is conveyed to, and combined with, feed stream 3 to the first-pass membrane unit 34.
  • This configuration potentially affords reduced energy use and allows for use of a smaller solids separation device than the embodiment shown in Fig. 1.
  • the second fraction stream 16 containing a minority ( ⁇ 50%) of mass and volume flow rate of stream 7 is conveyed to the solids separation device 8.
  • the solids separation device 8 e.g., gravity settling tank, centrifuge, hydrocyclone or filter
  • the amount of solids leaving the desalination system in minority fraction stream 15 from the solids separation unit 8 is controlled so that the mass of solids leaving the desalination method in minority fraction stream 15 and in permeate stream 14 from the second-pass membrane separation unit 34 is equal to the mass of solids entering the system as a part of feed stream 1.
  • a comminution device (not shown in Fig. 2), such as shear mixer or gear pump, may be placed majority fraction stream 32.
  • FIG. 3 Another embodiment of the present invention is shown in Fig. 3.
  • This embodiment is the same water desalination method as shown in Fig. 1 but with the addition of splitting the system feed stream 1 into two fractions.
  • the first fraction 2 is conveyed to, and combined with, permeate stream 9 from the first-pass membrane separation unit 33 to form feed stream 30 to the second pass membrane separation unit 34.
  • the second fraction of the system feed stream 1 is combined with stream 13 and majority fraction stream 32 to form feed stream 3 to the first-pass membrane separation unit 33.
  • the advantage of operating the desalination method in this configuration is that a portion of the system feed bypasses the first-pass membrane separation unit 33 and is fed directly into the second-pass membrane separation unit 34. Such a configuration potentially reduces energy use and allows for use of a smaller first-pass membrane separation unit than is the case for the embodiment shown in Fig. 1.
  • the flow rate of stream 2 depends on the concentration of sparingly soluble solutes in stream 2 and in stream 9 and the recovery rate at which the second-pass membrane unit 34 is operated.
  • concentration level of sparingly soluble solutes in stream 9 depends on the rejection rate of the first-pass membrane 5 for the solutes. Use of this Fig. 2 configuration is limited to cases where the rejection rate achieved by the first-pass membrane 5 for sparingly soluble solutes is high enough that system feed water 2 can be directly blended into stream 9 without exceeding the concentration limit at which fouling may occur on membrane 11 given the recovery rate at which second- pass membrane separation unit 34 is operated.
  • FIG. 4 Another embodiment of the present invention is shown in Fig. 4.
  • This embodiment is the same water desalination method as shown in Fig. 1 but with the addition of heating means 26 for heating the desalination system feed stream 1 using an external heat source 35.
  • the heating means 26 used to heat the system feed stream 1 could be, for example, a heat exchanger or a salinity gradient solar pond.
  • the heat source could be, for example, heat produced by burning carbonaceous fuels, waste heat from other operations, or solar radiation.
  • the desired effect of this embodiment of the present invention is to increase the temperature of the desalination system feed stream 1 so that the temperature of stream 31 after being heated is 10°C to 40°C higher than the ambient temperature of the system feed stream 1.
  • the first-pass membrane 5 and the second-pass membrane 11 will be able to operate at 40% to 60% higher flux rates than the flux rates achieved when the ambient system feed stream 1 temperature is, for example, 18°C.
  • Such improved membrane flux rates reduce energy use and lower capital costs.
  • FIG. 5 Another embodiment of the present invention is shown in Fig. 5.
  • This embodiment is the same water desalination system shown in Fig. 2 but with the addition of means for (i) splitting minority fraction stream 15 (the stream containing the high level of suspended solids) leaving solids separation device 8 into two fractions (a recovery stream 21 and a discharge stream 22); and (ii) splitting majority fraction stream 32 (the stream containing the lower level of suspended solids) leaving the solids separation device 8 into two fractions (a recovery stream 18 and a discharge stream 19).
  • solids separation device 8 whose operation can be instantaneously adjusted and controlled, such as a hydrocyclone or centrifuge, is preferred.
  • the first fraction of the split stream with a high level of suspended solids, namely discharge stream 22, is discharged from the system, while the second, recovery fraction 21 is returned to, and combined with, the streams comprising the feed stream 3 to the first-pass membrane unit.
  • the first, discharge fraction 19 of the split stream with a low level of suspended solids 32 is discharged from the system.
  • the second, recovery fraction 18 is returned to, and combined with, the streams comprising the feed stream 3 to first-pass membrane unit.
  • FIG. 6 Still another embodiment of the present invention is shown in Fig. 6.
  • This embodiment is the same system and method shown in Fig. 5 but with the addition of desupersaturating means 28 for desupersaturating the solutions containing the preferential precipitation nucleation crystals (streams 17, 18 and 21 in Fig. 6) before the crystals are reused in the process.
  • the means for desupersaturation in this embodiment may consist of, for example, reactor vessel with a mechanical stirrer 60.
  • the solution containing the nucleation crystals is conveyed along line 23 and combined with the system feed stream 1 to form the feed stream 3 to the first-pass membrane separation unit 33.
  • the desired effect of providing the desupersaturating means 28 as part of the present desalination system and method is to allow a greater fraction of the crystals to exist in suspension, as opposed to being dissolved in a supersaturated solution, before the crystals are returned to, and reused in, the first-pass membrane separation unit 33.
  • FIG. 7 Another embodiment of the present invention is shown in Fig. 7. This embodiment is the same water desalination system shown in Fig. 5 but with the addition of adjustment means 29 for reducing the agronomic sodium adsorption ratio of the permeate stream 14 from the second-pass membrane unit 34.
  • This embodiment is particularly useful in cases where the product water produced is used as agricultural irrigation water.
  • the permeate stream 14 from the second-pass membrane separation unit 34 will, in most cases, have an unfavorable ratio of sodium ions to the sum of calcium and magnesium ions. Because of this unfavorable ratio (computed as the so-called "sodium adsorption ratio" of the water), the product water will not penetrate into soil at an acceptable rate.
  • This deficiency exists because the reverse osmosis class of membranes, as typically used for membrane 11 in the second-pass membrane separation unit 34, characteristically reject a greater percentage of divalent ions (e.g., calcium and magnesium) than monovalent ions (e.g., sodium).
  • the adjusted product water 20 has more utility for use as agricultural irrigation water than permeate stream 14.
  • an on-farm treatment and recycling plant could be provided.
  • a computer model that would treat 15 gallons per minute (GPM) of agricultural drainage water.
  • the numbers shown below are consistent with what would be typical for a system of the present invention, but are intended for illustrative purposes only. No limitations on the invention should be inferred from this predictive model.
  • salinated water having a hardness of 2,061 mg/L (with TDS of 6,450 mg/L and a pH of 7.5) and the composition shown in TABLE I could be passed through a cartridge filter and split into a by-pass stream fed directly to a second semi- permeable membrane barrier, and a primary feed stream fed to a first semi-permeable membrane barrier.
  • the first semi-permeable membrane barrier apparatus in this embodiment could be a two-stage tubular nanofiltration apparatus consisting of nine (9) parallel pathways of Vi" diameter tubular membranes with a total path length of 864 feet followed by 5 parallel pathways of W diameter tubular membranes with total path length of 864 feet.
  • the tubes are contained in modules to create this flow pattern.
  • the feed would be, of course, pressurized. , Pressurization could be achieved either through a raised, gravity- released feed tank or pumps, or any combination thereof.
  • the total membrane area of this embodiment for the first semi-permeable membrane would be 1,574 ft 2 . In this embodiment, some of the permeate stream from the first stage could bypass the second stage.
  • the permeate stream from the first semi-permeable membrane apparatus would be sent to the second semi- permeable membrane barrier, and (in this example embodiment) the retentate stream would be split into two streams, namely a majority fraction which would be sent to a desupersaturation device, and a minority fraction stream which would be sent to a solids separation device.
  • the solids separating device would be a hydrocyclone.
  • the desupersaturation reactor vessel would be a 300 gallon stirred tank vessel.
  • the output from the desupersaturation vessel would be sent back to the feed to the first semi-permeable membrane barrier device.
  • the output stream from the solids separation device (as noted above, for example with respect to FIG. 5) would be split into two streams.
  • the discharge fraction in this embodiment would produce over 100 pounds of gypsum per day.
  • the second semi-permeable membrane barrier of this embodiment would be a reverse osmosis device (spiral-type) comprised of a 20 foot long 3x6 array of 4" x 40" elements (18 elements total).
  • the feed stream would be pressurized. This could be done, as above, with both a gravity feed tank and booster pump.
  • the permeate stream from the second semi- permeable membrane barrier device (spiral RO) would have a TDS content of 149 mg/L.
  • Table II The compositional breakdown of such a stream under such conditions is summarized in Table II below.
  • the RO permeate stream can be modified by adding content from the discharge fraction of the solids separating device (namely, gypsum). If this was done, an adjusted product water stream could be achieved having a TDS of 270 mg/L and a compositional breakdown as summarized in Table III.
  • sparingly soluble constituents include carbonates, silicates, sulfates, phosphates, fluorides and hydroxides of metals such as aluminum, barium, calcium, magnesium, strontium, chromium, copper, lead, nickel, silver, tin, titanium, vanadium, zinc and other multivalent cations of the periodic table.
  • Other soluble constituents that may be treated include the salts of organic materials such as, for example, carboxylic acids, polymeric compounds (polyelectrolytes that may exist in salt forms), alcohols and hydrocarbons. The salts are formed when the sparingly soluble constituents are concentrated and precipitate out of solution to form mineral scale deposits on the membrane surface on the high pressure side of the membrane.
  • concentration at which precipitation occurs depends on the solubility limit of the specific salt and the conditions present in the system (e.g., temperature, pH, and TDS level).
  • concentration at which precipitation occurs depends on the solubility limit of the specific salt and the conditions present in the system (e.g., temperature, pH, and TDS level).
  • highly soluble salts will pass through the membrane and, therefore, will not precipitate and form mineral scale on the membrane surface.

Abstract

La présente invention concerne un système et un procédé de dessalement d'une solution à traiter contenant un niveau élevé de solutés modérément solubles, tels que le sulfate de calcium, dans lesquels un fort pourcentage de la teneur en eau de la solution à traiter est récupéré sous forme d'eau purifiée. Le procédé et le système consistent à introduire une quantité suffisante de cristaux de nucléation sur le côté basse pression d'une unité de séparation de premier passage de sorte que les solutés modérément solubles précipitent sur les cristaux de nucléation en suspension, plutôt que sur la surface de la membrane-barrière semi-perméable de premier passage. Le perméat issu de l'unité de séparation à membrane de premier passage est ensuite envoyé au côté haute pression d'une deuxième unité de séparation à membrane de deuxième passage. La membrane-barrière semi-perméable de deuxième passage rejette les solutés dissous additionnels, dont une partie peut être renvoyée à la membrane de premier passage, de manière à ce que le perméat ayant un faible niveau de solutés dissous soit produit sur le côté basse pression de la membrane-barrière de deuxième passage.
PCT/US2004/009055 2003-03-24 2004-03-24 Systeme et procede de membrane a precipitation preferentielle WO2004085040A2 (fr)

Applications Claiming Priority (4)

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US45707403P 2003-03-24 2003-03-24
US60/457,074 2003-03-24
US10/807,044 2004-03-23
US10/807,044 US20050016922A1 (en) 2003-03-24 2004-03-23 Preferential precipitation membrane system and method

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WO2004085040A3 WO2004085040A3 (fr) 2005-03-31
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KR102531484B1 (ko) 2015-06-24 2023-05-10 포리페라 인코포레이티드 정삼투를 통한 알콜성 용액의 탈수 방법 및 관련 시스템
WO2017115378A1 (fr) * 2015-12-30 2017-07-06 Ora Kedem Procédé et système pour osmose inverse à récupération élevée
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